CN101218320B - Method for processing hydrocarbon pyrolysis effluent - Google Patents
Method for processing hydrocarbon pyrolysis effluent Download PDFInfo
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- CN101218320B CN101218320B CN2006800247671A CN200680024767A CN101218320B CN 101218320 B CN101218320 B CN 101218320B CN 2006800247671 A CN2006800247671 A CN 2006800247671A CN 200680024767 A CN200680024767 A CN 200680024767A CN 101218320 B CN101218320 B CN 101218320B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/002—Cooling of cracked gases
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/14—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in pipes or coils with or without auxiliary means, e.g. digesters, soaking drums, expansion means
- C10G9/18—Apparatus
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
- F28D7/16—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/301—Boiling range
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
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- Oil, Petroleum & Natural Gas (AREA)
- Thermal Sciences (AREA)
- Physics & Mathematics (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
A method is disclosed for treating the effluent from a hydrocarbon pyrolysis process unit to recover heat and remove tar therefrom. The method comprises passing the gaseous effluent to at least one primary heat exchanger, thereby cooling the gaseous effluent and generating high pressure steam. Thereafter, the gaseous effluent is passed through at least one secondary heat exchanger having a heat exchange surface maintained at a temperature such that part of the gaseous effluent condenses to form in situ a liquid coating on said surface, thereby further cooling the remainder of the gaseous effluent to a temperature at which tar, formed by the pyrolysis process, condenses. The condensed tar is then removed from the gaseous effluent in at least one knock-out drum.
Description
The cross reference of related application
The application expressly is herein incorporated by reference whole disclosures of following application: introduce attorney 2005B060, title is " method of cooling of hydrocarbon pyrolysis effluent "; Attorney 2005B062, title are " working method of hydrocarbon pyrolysis effluent "; Attorney 2005B063, title are " working method of hydrocarbon pyrolysis effluent "; Attorney 2005B064, title are " working method of hydrocarbon pyrolysis effluent "; With attorney 2005B065, title is " working method of hydrocarbon pyrolysis effluent "; They all are hereby incorporated by and submit to simultaneously with the application.
Invention field
The present invention relates to working method from the gaseous state ejecta of hydrocarbon pyrolysis installation.
Background of invention
Prepare light olefin (ethene, propylene and butylene) by various hydrocarbon feeds and use pyrolysis or steam cracking technology.Pyrolysis comprises raw material is heated to fully and causes more macromolecular thermolysis.
In the steam cracking process, it is desirable from the technology ejecta materials flow of leaving pressure still, farthest reclaiming useful heat.The efficient recovery of this heat is one of principal element of steam cracker energy efficiency.
Yet the steam cracking process also produces the molecule that tends to combine to form high molecular weight material (being called as tar).Tar is high boiling point adhesive reaction property material, and it can make the heat-exchange equipment fouling under certain condition, causes heat exchanger failure.Fouling tendency can have three state of temperature characteristics.
On hydrocarbon dew point (temperature of the first drop of liquid condensation), fouling tendency is relatively low.The gas phase fouling is not serious usually, and does not have the liquid that possibly cause fouling.The interchanger of appropriate designs (normally transfer line exchanger) therefore can be under this state in the situation recover heat of minimum fouling.
Between the temperature of hydrocarbon dew point and steam-cracked tar total condensation, fouling tendency is high.In this state, the components condense of heavy in the materials flow.These components are considered to be clamminess and/or viscosity, and this causes that they are attached on the surface.In addition, in case this material is attached on the surface, it will experience and make its sclerosis and make it more be difficult to the thermal destruction of removing.
Under the temperature that is equal to or less than the steam-cracked tar total condensation, fouling tendency is relatively low.In this state, condensed material is enough mobile, and with easily mobile under processing condition, and fouling is not serious problem usually.
Being used for the cool pyrolysis unit ejecta adopts interchanger then to adopt the water quench tower with a kind of technology of removing gained tar, in this water quench tower, removes condensables.When cracking light gas (mainly being ethane, propane and butane), verified this technology is effectively, because the cracker (being referred to as gas conveter) of processing lightweight material produces more a spot of tar.As a result, interchanger can reclaim most of valuable heat effectively and non flouling behaviour and more a spot of tar can be separated by the water quenching, even some difficulties are arranged.
Yet, this technology for pressure naphtha and more the steam cracker of heavy feed stock (being referred to as liquid cracker) to use be not satisfied because liquid cracker produces the tar more much more than gas conveter.Interchanger can be used for from the liquid cracking, removing some heat, but only reduces to the temperature that tar begins condensation.Under this temperature, can not use conventional interchanger, because they will be by the gathering of the tar on the heat exchanger surface and thermal destruction and fouling promptly.In addition, when the pyrolysis effluent from these raw materials was carried out quenching, some heavy oil that produced and tar had with the roughly the same density of water and can form stable oil/water miscible liquid.In addition, the more a large amount of heavy oil and the tar that produce through the liquid cracking will cause the water quench operation to lose efficacy, and this makes that being difficult to from water of condensation, produce steam handles excessive quench water and heavy oil and tar with being difficult to by acceptable manner on the environment.
Therefore, in most of commercial liquid crackers, use transfer line exchanger system, primary fractionator and water quench tower or indirect condenser to realize usually from the cooling of the ejecta of pressure still.For typical feed naphtha; Transfer line exchanger with process stream be cooled to about 700
(370 ℃), can be used for other local extra high pressure steam of technology thereby produce effectively.Primary fractionator be commonly used to tar condensing with tar is separated with light weight fluid cut (being called pyrolysis gasoline) more, and be used for reclaiming about 700
(370 ℃) and about 200
heat between (90 ℃).The gas streams that water quench tower or indirect condenser further will leave this primary fractionator be cooled to about 104
(40 ℃) so that the most of dilution steam generation condensation that exists with pyrolysis gasoline is separated with the gaseous state olefinic product, then it is delivered to compressor.
Yet primary fractionator is a very complicated equipment, and it generally includes oily quenching part, primary and one or more oil outer pumparound loops.In the quenching part; Add quenching oil with the ejecta stream cools to about 400-554
(200-290 ℃), thereby condensation is present in the tar in this materials flow.In primary, the tar of condensation separates with the remainder of this materials flow, in one or more pump circulations district, removes through turning oil and reduces phlegm and internal heat and in one or more distillation zones, pyrolysis naphtha is separated with heavier substances more.In one or more external pumparound loops, use indirect heat exchanger will turn back to this primary fractionator or direct quench point then from the oil cooling that primary fractionator is discharged.
Primary fractionator with relative pump circulation is a member the most expensive in the whole cracking system.Primary itself is an one piece apparatus maximum in the technology, and usually for medium-sized liquid cracker, its diameter is about 25 feet, highly above 100 feet.This tower is bigger, because its in fact two kinds of minor components of fractionation, i.e. tar and pyrolysis gasoline in the presence of a large amount of low-pressure gases.Pumparound loops is bigger equally, under the situation of medium-sized cracker, per hour handles the turning oil above 300 ten thousand Pounds Per Hours.Interchanger in the pumparound circuit must be bigger, and reason is high flow capacity, reclaims the heat necessary tight temperature difference (temperature approach) with useful level, and the tolerance limit of fouling.
In addition, primary fractionator has many other restriction and problems.Specifically, heat passage generation twice, promptly from gas to the tower inner pumparound liquid then from this pumparound liquid to the externally cooled facility.This in fact need be to the investment of two heat exchange systems, and to removing two temperature difference of heat request (or residual quantity), thereby reduce thermo-efficiency.
In addition, although between tar and the gasoline stream fractionation takes place, these two kinds of materials flows are further processing usually.Sometimes, need carry out stripping removing light component to tar, and gasoline possibly carry out fractionation again to reach its end point specification.
In addition, primary is easy to fouling with its pumparound loops.Coke is assembled and must in the overhaul of the equipments process, finally be removed at the base section of this tower.Pumparound loops also receives scale effect, thereby need from strainer, remove the interchanger of coke and periodic cleaning fouling.Column plate in the tower and filler receive scale effect sometimes, and this maybe limiting device production.System also contains the flammable liquid hydrocarbons of remarkable storage, and this is undesirable from the inherent safety viewpoint.
The present invention manages to be provided for handling the pyrolysis installation ejecta; Especially from the simplified method of the steam cracking ejecta of petroleum naphtha, this method makes the recovery maximization of useful heat energy and can not make cooling apparatus fouling and this method get rid of the needs to primary and utility appliance thereof.
USP 4,279,733 and 4,279,734 have proposed to use the cracking method of expander, indirect heat exchanger and fractionator cooling ejecta, and said ejecta is produced by steam cracking.
USP 4,150,716 and 4,233,137 have proposed to comprise the heat recovery equipment of pre-cooling zone, heat recovery area and disengaging zone; Wherein in pre-cooling zone, let the ejecta that produces by steam cracking contact with the quenching oil of injection.
People's such as Lohr " Steam-cracker Economy Keyed toQuenching "; Oil&Gas Journal; The 76th volume (the 20th phase); 63-68 page or leaf (1978) has proposed the two-stage quenching, it comprise with the indirect quenching of transfer line exchanger with produce HP steam and with the direct quenching of quenching oil to produce MP steam.
USP 5; 092; 981 and 5; 324,486 have proposed to be used for the two-stage method of quenching of the ejecta that produced by steam cracker furnace, and it comprises: be used for cooling off rapidly stove ejecta and the primary transfer line exchanger that produces high-temperature steam and be used for the stove ejecta be cooled to low as far as possible to effective primary fractionator or quench tower performance consistent temperature and in producing to the secondary transfer line exchanger of LP steam.
USP 5,107,921 have proposed to have different transfer line exchanger of managing a plurality of tube sides of diameters.USP 4,457,364 have proposed close-connected transfer line exchanger device.
USP 3,923,921 have proposed the petroleum naphtha process for steam cracking, and it comprises that letting ejecta pass transfer line exchanger passes quench tower after cooling off this ejecta.
WO 93/12200 has proposed as follows will be from the method for the gaseous state ejecta quenching of hydrocarbon pyrolysis installation; Let this ejecta pass transfer line exchanger; With liquid water this ejecta quenching is made when this ejecta gets into main separation vessel then; With this ejecta be cooled to 220
-266
temperature of (105 ℃-130 ℃), make heavy oil and tar condensing.In this main separation vessel, the oil of this condensation is separated with the gaseous state ejecta with tar and let remaining gaseous state ejecta flow in the quench tower, the temperature with this ejecta is reduced to the chemically stable level of this ejecta there.
EP205205 has proposed to have two or more independently the transfer line exchanger cooling fluid of heat exchange section such as methods of cracked reaction product through use.
USP 5,294,347 propose in ethylene producing device, and the water quench column cools is left the gas of primary fractionator; And in many devices, the raw material that does not use primary fractionator and be fed into the water quench column is directly from transfer line exchanger.
JP 2001-40366 has proposed to cool off the mixed gas in high temperature range with vertical exchanger then with horizontal interchanger, and the heat exchange planes of said vertical exchanger is by the vertical direction setting.Pass through the heavy component of condensation in this vertical exchanger of fractionation by distillation of downstream refinement step afterwards.
WO 00/56841; GB 1,390, and 382; GB 1,309,309 with USP 4,444,697; 4,446,003; 4,121,908; 4,150,716; 4,233,137; 3,923,921; 3,907,661 and 3,959,420 have proposed to be used for the various device of thermally splitting gaseous stream quenching, wherein let the hot gaseous materials flow through wherein having injected the quenching pipeline or the quench tube of liquid coolant (quenching oil).
Summary of the invention
In one aspect, the present invention relates to be used for the treatment process from the gaseous state ejecta of hydrocarbon pyrolytic process device, this method comprises:
(a) let this gaseous state ejecta pass at least one main heat exchanger, thereby cool off this gaseous state ejecta and produce HP steam;
(b) let the gaseous state ejecta from step (a) pass the auxiliary heat exchanger that at least one has heat exchange surface; This heat exchange surface maintains and makes a part of condensation of this gaseous state ejecta with under the temperature that forms liquid coating on the said surface, thereby further the remainder of this gaseous state ejecta is cooled to make the temperature of the tar condensing that is formed by pyrolytic process; With
(c) tar with this condensation separates with the gaseous state ejecta.
In a preferred embodiment; With said heat exchange surface maintain less than about 599
under the temperature of (315 ℃), for example maintain under the temperature of about 300-500
(149 ℃-260 ℃).
In one aspect of the method, the present invention relates to be used for the treatment process from the gaseous state ejecta of hydrocarbon pyrolytic process device, this method comprises:
(a) let this gaseous state ejecta pass at least one main heat exchanger, thereby cool off this gaseous state ejecta and produce HP steam;
(b) let the said gaseous state ejecta from step (a) pass the auxiliary heat exchanger that at least one has heat exchange surface; This heat exchange surface maintains and makes a part of condensation of this gaseous state ejecta with under the temperature that forms liquid coating on the said surface, thereby further the remainder of this gaseous state ejecta is cooled to make the temperature of at least a portion condensation of the tar that is formed by pyrolytic process in said gaseous state ejecta;
(c) let the ejecta from step (b) pass at least one knockout drum, there, the tar of condensation separates with the gaseous state ejecta; And then
(d) will be reduced to from the temperature of the gaseous state ejecta of step (c) less than 212
(100 ℃); This method is carried out under the situation of primary fractionator not having.
In aspect another, the present invention relates to hydrocarbon cracking equipment, it comprises:
(a) be used for hydrocarbon feed pyrolytic reactor drum, this reactor drum has outlet, and the gaseous state pyrolysis effluent can leave this reactor drum via this outlet;
(b) in these reactor outlet downstream and connected at least one main heat exchanger, this main heat exchanger is used to cool off this gaseous state ejecta;
(c) in these at least one main heat exchanger downstream and connected at least one auxiliary heat exchanger; This auxiliary heat exchanger is used for further cooling off said gaseous state ejecta; Said at least one auxiliary heat exchanger has heat exchange surface; This heat exchange surface in use maintains and makes a part of condensation of this gaseous state ejecta with under the temperature that forms liquid coating on the said surface, thereby the remainder of this gaseous state ejecta is cooled to make the temperature of at least a portion condensation of the tar that is formed by pyrolytic process in the said gaseous state ejecta; With
(d) with the tar and the isolating device of gaseous state ejecta of this condensation.
The accompanying drawing summary
Fig. 1 is the indicative flowchart of handling according to an embodiment of the invention from the method for the cracked gaseous state ejecta of feed naphtha.
Fig. 2 is the sectional view of a pipe that is used for the wet transfer line exchanger of method shown in Figure 1.
Fig. 3 is the sectional view of inlet transition piece that is used for the shell-tube type wet transfer line exchanger of method shown in Figure 1.
Fig. 4 is the sectional view of inlet transition piece that is used for the tube-in-tube wet transfer line exchanger of method shown in Figure 1.
The detailed description of embodiment
The invention provides low-cost processes method, thereby from this materials flow, remove and reclaim heat and the C in this ejecta from the gaseous state ejecta materials flow of hydrocarbon pyrolysis reactor
5+ hydrocarbon and required C
2-C
4Alkene separates, and does not need primary fractionator and the fouling that is caused by tar of cooling apparatus is minimized.
Usually; The ejecta that is used for the inventive method through will about 104
-about 356
ebullient hydrocarbon feed in the TR of (40 ℃-about 180 ℃), pyrolysis prepares like petroleum naphtha.Temperature at the gaseous state ejecta in pyrolysis reactor exit is typically about 1400
-about 1706
(760 ℃-about 930 ℃) and the invention provides said ejecta is cooled to make required C
2-C
4The method of temperature that alkene can effectively compress is generally less than about 212
(100 ℃) are for example less than 167
(75 ℃) are for example less than 140
(60 ℃) are generally 68
-122
(20-50 ℃).
Specifically, the present invention relates to the treatment process from the gaseous state ejecta of petroleum naphtha cracking unit, this method comprises lets this ejecta pass at least one main heat exchanger, and this main heat exchanger can reclaim heat it is reduced to the temperature that fouling begins from this ejecta.If desired, can pass through the steam decoking, steam/air decoking or mechanical cleaning periodically clean this interchanger.Can the indirect heat exchanger of routine such as double-pipe exchanger or shell and tube heat exchanger be used for this facility.This main heat exchanger make water as heat-eliminating medium with process stream be cooled to about 644
-about 1202
(340 ℃-about 650 ℃); For example about 700
temperature of (370 ℃); And the generation extra high pressure steam, pressure is usually under about 1500psig (10400kPa).
When leaving said main heat exchanger, refrigerative gaseous state ejecta is still under the temperature greater than the hydrocarbon dew point (temperature of the first drop of liquid condensation) of this ejecta.For the typical feed naphtha under some cracking conditions, the hydrocarbon dew point of ejecta materials flow be about 581
(305 ℃).On this hydrocarbon dew point, fouling tendency is relatively low, i.e. vapor phase fouling is not serious usually, and does not have the liquid that possibly cause fouling.
After leaving said main heat exchanger; Then let said ejecta flow at least one auxiliary heat exchanger; This auxiliary heat exchanger makes it comprise heat exchange surface through design and operation, and this heat exchange surface is as cold as to be enough to produce the liquid hydrocarbon film with a part of condensation of this ejecta with at this heat exchange surface place.This liquid film be produce on the spot and preferably be equal to or less than the temperature that makes the tar total condensation; Usually about 302
-about 599
under (150 ℃-about 315 ℃), for example about 446
under (230 ℃).This suitable selection through heat-eliminating medium and design of heat exchanger is guaranteed.Because heat passage main resistance is between bulk process stream and film, this film can be in than under the remarkable low temperature of bulk stream.When bulk stream was cooled, this film kept heat exchange surface moistening by fluid materials effectively, thereby prevents fouling.This kind auxiliary heat exchanger must be cooled to this process stream to produce the temperature of tar continuously.If before this point, stop cooling, then fouling takes place probably, and reason is that this process stream possibly still be in fouled condition.
Through after the auxiliary heat exchanger, said refrigerative ejecta is supplied with tar knock-out drum, the tar of condensation separates with the ejecta materials flow there.If necessary, can a plurality of knockout drums be connected in parallel, make single drum can stop using and when device is being operated, clean.The tar of removing in this stage of this technology have usually at least 302
initial boiling point of (150 ℃).
The ejecta that gets into tar knock-out drum should be under enough low temperature; Usually about 3024
(150 ℃)-about 599
under (315 ℃); For example about 446
under (230 ℃), so that tar promptly separates in this knockout drum.Therefore, depend on the manipulation strength of interchanger, the ejecta materials flow can further be cooled off through direct injection less water after it flows through from interchanger and before it gets into tar knock-out drum.
In tar knock-out drum, remove after the tar; Additional cooling program is implemented in materials flow to said gaseous state ejecta; Like this; From this ejecta, reclaim additional heat energy and the temperature of this ejecta is reduced to light alkene can be by the temperature of effective compression in this ejecta; Common 68
-122
(20-50 ℃), preferably approximately 104
(40 ℃).Additional cooling program comprises lets this ejecta pass one or more cracked gas cooler, passes water quench tower or at least one indirect fractional distillating tube then, so that with pyrolysis gasoline in this ejecta and water condensation.Then condensate separation is become water-based cut and pyrolysis naphtha and with this pyrolysis naphtha distillation to reduce its full boiling point.Usually; By the pyrolysis naphtha of this ejecta materials flow condensation have less than 302
initial boiling point of (150 ℃) and surpass 500
(260 ℃); For example about 842
full boiling point of (450 ℃), and it has the full boiling point of 400-446
(200-230 ℃) usually after distillation.
Therefore will find in the method for the invention, said pyrolysis effluent will be cooled to the temperature that light alkene in the ejecta can not carried out fractionating step by effective compression.Therefore, method of the present invention is got rid of the needs to primary fractionator (conventional petroleum naphtha cracking unit heat removal system expensive component).As a result, pyrolysis naphtha comprises some than heavy component, if whole gaseous state ejecta has passed primary fractionator, and then more said maybe not can than heavy component the existence.Yet, in simple distillation tower (generally including 15 column plates, a reboiler and a condensing surface), remove these than heavy component, this distillation tower can be built by the price of conventional primary fractionator part.
Except the investment and process cost of the reduction relevant with not using primary fractionator, method of the present invention has also realized some advantages.Use at least one main heat exchanger and at least one auxiliary heat exchanger to make and reclaim hot value maximization.In addition, after isolating tar, reclaim additional useful heat.In special container, from technology, remove tar and coke as soon as possible, thereby fouling is minimized and simplify from the coke of this technology and remove.Reduce liquid hydrocarbon inventory widely, got rid of the pump circulation pump simultaneously.The fouling of primary fractionator trays and pumparound exchangers is eliminated.If the flaring in the time of can reducing SV and separate removal rates and relevant cold water or power failure and take place.
When additional cooling program comprises when letting ejecta pass at least one indirect fractional distillating tube; Be provided with aptly with the temperature with ejecta be reduced to about 68
-about 122
(20 ℃-about 50 ℃), usually about 104
(40 ℃).Through operation under a kind of like this low temperature; About 176
that reach with common employing water quench tower temperature of (80 ℃) compares; Can the additional light hydrocarbon of condensation, thus the separating of the density that reduces hydrocarbon phase and improvement pyrolysis gasoline and water.This kind separation takes place in the sedimentation rotary drum usually.
In order further to reduce the density of condensation of hydrocarbons, one embodiment of the invention are considered light pyrolysis gasoline is added in the pyrolysis gasoline stream of condensation.Several kinds of light fractions of pyrolysis gasoline produce in naphtha steam cracker usually, for example, mainly comprise C
5With lightweight C
6The cut of component and benzene enriched material cut.These cuts have the density lower than the pyrolysis gasoline stream of whole condensation.This kind materials flow is added in the pyrolysis gasoline stream of condensation and will be reduced its density, thereby improve separating of hydrocarbon phase and water.The ideal recycle fraction will make the density of the pyrolysis gasoline of condensation reduce maximization under the evaporation of minimum.Can it directly be added in quench water settler or the upstream position.
The low level heat of in one embodiment of the invention, will the gaseous emission from cracked gas cooler removing is used for the feedwater of heat de-airing device.Usually; Use in the degasser LP steam with softening water and steam condensate be heated to about 266
(130 ℃), be removed in this degasser air.In order to realize effective stripping; The top temperature that will get into the water of this degasser usually be limited to 20
below the degasser temperature-50
(11-28 ℃), this depends on the design of deaerator system.This allows the use of the cooling cracked gas stream by indirect heat exchange to heat the water to 212
-239
(100 ℃ -115 ℃).Cooling water heat exchanger can use cracked gas stream is replenished cooling as required.For instance; In a commercial olefins plant, current use 242klb/hr LP steam will 84
about 816klb/hr softening water under (29 ℃) and 167
849klb/hr steam condensate under (75 ℃) be heated to 268
(131 ℃).The heat that use is reclaimed from cracked gas maybe be potentially with these materials flows be heated to 241
(116 ℃).This can need be reduced to 46klb/hr from 242klb/hr with deaerator steam, has practiced thrift the 196klb/hr LP steam, and can the cooling tower load be reduced about 189MBTU/hr.
To the present invention more specifically be described with reference to accompanying drawing at present.
With reference to Fig. 1 and 2, shown in method in, the hydrocarbon feed 10 that will comprise petroleum naphtha is supplied with steam cracking reaction devices 12 with dilution steam generation 11, there the hydrocarbon feed heating is produced the hydrocarbon of lower molecular weight to cause this raw material thermolysis, for example C
2-C
4Alkene.Pyrolytic process in this steam cracking reaction device has also produced some tar.
The gaseous state pyrolysis effluent 13 that leaves this steam cracker furnace passes at least one primary transfer line exchanger 14 at first, this interchanger with this ejecta be cooled to about 700
(370 ℃).After leaving this main heat exchanger 14; Then at least one auxiliary heat exchanger 16 is supplied with in refrigerative ejecta materials flow 15; Wherein on the pipe side of this interchanger 16 with this ejecta be cooled to about 446
(230 ℃), simultaneously on the shell-side of this interchanger 16 with oiler feed 18 (Fig. 2) from about 261
(127 ℃) be preheating to about 410
(210 ℃).Like this, the heat exchange surface of interchanger 16 is enough cold to produce liquid film 19 on the spot with the surface at this pipe, and this liquid film is produced by the condensation of this gaseous state ejecta.
Though Fig. 2 described ejecta materials flow 15 and oiler feed 18 concurrent flow so that the temperature of process side ingress liquid film 19 minimize; But other arrangement of mobile also is possible, comprises counter-current flow.Because heat passage is rapidly between oiler feed and tube metal, so this tube metal of any point place in interchanger 16 is only than oiler feed 18 low-grade fevers.Heat passage also is rapidly between tube metal on the process side and liquid film 19, therefore in interchanger 16 this film temperature of any point place only than tube metal temperature low-grade fever.Whole length along interchanger 16; This film temperature be usually less than about 446
(230 ℃), promptly tar under these conditions fully by the temperature of this specified raw material condensation.Guaranteed that like this this film is mobile fully, and therefore avoided fouling.
In interchanger 16, be the most effectively one of purposes of the heat that produces in the pyrolysis installation with the high pressure boiler water supply preheating.After the degassing, can obtain usually about 261
oiler feed under (127 ℃).Therefore oiler feed from degasser can be carried out preheating and be sent at least one primary transfer line exchanger 14 afterwards in wet transfer line exchanger 16.Being used for all heat of preboiler feedwater will increase high pressure steam production.
When leaving interchanger 16, refrigerative gaseous state ejecta makes under the temperature of tar condensing and is getting at least one tar knock-out drum 20 then, and this ejecta is separated into tar and coke fraction 21 and gaseous fraction 22 there.
Afterwards; Gaseous fraction 22 passes one or more fractional distillating tubes 23 and 25; There; This cut through with degasser feedwater then with indirect heat transfer as the water coolant of heat-eliminating medium be cooled to about 68
-about 122
(20 ℃-about 50 ℃), for example about 104
temperature of (40 ℃).Then refrigerative ejecta (pyrolysis gasoline and the water that comprise condensation) is mixed with light pyrolysis gasoline stream 29 and let it flow to quench water settling drum 30.In this settling drum 30; Condensate separation becomes hydrocarbon-fraction 32, water-based cut 31 and gaseous overhead 33; This hydrocarbon-fraction 32 is supplied to distillation tower 27, and this water-based cut 31 is supplied to sour water stripping (SWS) tower (not shown), and this gaseous overhead 33 can directly be supplied to compressor.In distillation tower 27; Hydrocarbon-fraction 32 is fractionated into pyrolysis naphtha 34 and steam cracked gas oil fraction 35; This pyrolysis naphtha 34 has the full boiling point of 356-446
(180-230 ℃) usually, and this steam cracked gas oil fraction 35 has the full boiling point of 500-1004
(260-540 ℃) usually.
The hardware that is used for interchanger 16 can be similar with the hardware of the secondary transfer line exchanger that is generally used for gas cracking facility.Can use tube and shell heat exchanger.Can on the pipe side, process stream be cooled off by one way stationary tubesheet layout.The coke that relatively large caliber will allow the upper reaches to produce can not stop up through this interchanger.The design of interchanger 16 can minimize temperature and makes the thickness maximization of liquid film 19 through setting, for example, and through realizing on the outside surface that burr is added to Tube Sheet of Heat Exchanger.Can on shell-side, press single pass arrangement with the oiler feed preheating.Perhaps, shell-side can be changed with pipe side facility.Can use and stream or counter-current flow, as long as keep enough low along the film temperature of this interchanger length.
The inlet transition piece of the shell-tube type wet transfer line exchanger that for example, is fit to is shown in Fig. 3.Tube Sheet of Heat Exchanger 41 is fixed in the hole 40 in the tube sheet 42.Pipe filler rod or lasso 45 are fixed in the hole 46 in the false tubesheet 44 with tube sheet 42 arranged adjacent, make lasso 45 stretch into Tube Sheet of Heat Exchanger 41, wherein thermoinsulating material 43 places between tube sheet 42 and the false tubesheet 44 and between Tube Sheet of Heat Exchanger 41 and the lasso 45.Adopt this layout, false tubesheet 44 is being operated under the temperature near the technology temperature in lasso 45 very much, and Tube Sheet of Heat Exchanger 41 is being operated under the temperature near coolant temperature very much.Therefore, seldom the fouling meeting takes place on false tubesheet 44 and lasso 45, and reason is that they operate on the pyrolysis effluent dew point.Similarly, seldom the fouling meeting takes place on the surface of Tube Sheet of Heat Exchanger 41, and reason is that it operates under less than the temperature that makes the tar total condensation.The transformation very rapidly that this layout provides the surface temperature aspect is to avoid at hydrocarbon dew point and to make the fouling temperature regime between the temperature of tar total condensation.
Perhaps, being used for the hardware of secondary transfer line exchanger can be similar with the hardware of close-connected primary transfer line exchanger.Can use double-pipe exchanger.Process stream can cool off in interior pipe.The coke that relatively large diameter of inner pipe will allow the upper reaches to produce can not stop up through this interchanger.Oiler feed can preheating in the annular space between outer tube and the interior pipe.Can use and stream or counter-current flow, as long as keep enough low along the film temperature of this interchanger length.
The inlet transition piece of the tube-in-tube wet transfer line exchanger that for example, is fit to is shown in Fig. 4.Heat exchanger entrance pipeline 51 is connected with swage 52, and this swage 52 is connected with oiler feed inlet 55.The annular space that insulating material 53 is filled between heat exchanger entrance pipeline 51, swage 52 and the oiler feed inlet 55.Tube Sheet of Heat Exchanger 54 is connected with oiler feed inlet 55, makes to exist little gap 56 to allow thermal expansion between the starting end of end and Tube Sheet of Heat Exchanger 54 of heat exchanger entrance pipeline 51.A kind of similar arrangements (although in the flow of process gases pipeline, having introduced three-way piece) is at USP 4,457, is described in 364.Whole heat exchanger entrance pipeline 51 is being operated under the temperature near technological temperature very much, and Tube Sheet of Heat Exchanger 54 is being operated under the temperature near the temperature of heat-eliminating medium very much.Therefore, seldom the fouling meeting takes place on the surface of heat exchanger entrance pipeline 51, and reason is that it operates on the pyrolysis effluent dew point.Similarly, seldom the fouling meeting takes place on Tube Sheet of Heat Exchanger 54, and reason is that it operates under less than the temperature that makes the tar total condensation.Equally, the transformation very rapidly that the surface temperature aspect is provided of this layout is to avoid at hydrocarbon dew point and to make the fouling temperature regime between the temperature of tar total condensation.
Can be orientated so that process fluid substantial horizontal, perpendicular upwards flow or preferred perpendicular flows downward auxiliary heat exchanger.The perpendicular system of flowing downward helps to guarantee that the liquid film that forms on the spot keeps quite even above the total inner surface of Tube Sheet of Heat Exchanger, thereby fouling is minimized.On the contrary, with horizontal alignment, because that the action of gravity liquid film will tend to will be thicker and at the top and thinner in Tube Sheet of Heat Exchanger bottom.With the perpendicular flow arrangement that makes progress, liquid film possibly tend to separate with tube wall, because gravity tends to pull liquid film downwards.Another actual cause that helps the perpendicular downflow orientation is that the inlet materials flow of leaving main heat exchanger is usually located at furnace construction top, and the outlet materials flow hopes to be in lower height.The auxiliary heat exchanger that flows downward will provide the height of this materials flow to change naturally.
Can design to allow using steam or steam and AIR MIXTURES to be the interchanger decoking auxiliary heat exchanger with stove decoking system.When using steam or steam and AIR MIXTURES as the stove decoking, the stove ejecta will at first pass through main heat exchanger and pass through auxiliary heat exchanger then, and will be treated then in decoking ejecta system.Adopt this characteristic, the internal diameter of auxiliary heat exchanger pipe is favourable more than or equal to the internal diameter of main heat exchange organ pipe.This any coke of having guaranteed to be present in the main heat exchanger ejecta will easily can not cause any restriction through the auxiliary heat exchanger pipe.
Though combined some embodiment preferred to describe the present invention, so that can more fully understand and understand all respects of the present invention, do not hoped to limit the invention to these specific embodiments.On the contrary, hope to contain all alternativess, modification and the equivalent in the scope of the invention that can be included in the appended claims qualification.
Claims (38)
1. be used for the treatment process from the gaseous state ejecta of hydrocarbon pyrolytic process device, this method comprises:
(a) let this gaseous state ejecta pass at least one main heat exchanger, thereby cool off this gaseous state ejecta;
(b) let the gaseous state ejecta from step (a) pass the auxiliary heat exchanger that at least one has heat exchange surface; This heat exchange surface maintains 300 ° of F to the temperature less than 599 ° of F; Make a part of condensation of this gaseous state ejecta on said surface, forming liquid coating, thereby further the remainder of this gaseous state ejecta is cooled to make the temperature of the tar condensing that forms by pyrolytic process; With
(c) tar with this condensation separates with the gaseous state ejecta.
2. the process of claim 1 wherein said heat exchange surface is maintained under the 300-500 ° of temperature between the F.
3. claim 1 or 2 methods, wherein said heat exchange surface are vertically arranged and through maintaining under the said temperature with the heat-transfer medium indirect heat exchange that flows through said at least one auxiliary heat exchanger downward vertically.
4. claim 1 or 2 method, wherein said heat exchange surface are through maintaining under the said temperature with the water indirect heat exchange, and the water that will in this at least one auxiliary heat exchanger, heat is as the heat exchange medium in this main heat exchanger.
5. the method for claim 3, wherein said heat exchange surface are through maintaining under the said temperature with the water indirect heat exchange, and the water that will in this at least one auxiliary heat exchanger, heat is as the heat exchange medium in this main heat exchanger.
6. claim 1 or 2 method, wherein step (c) comprises that the ejecta that lets from auxiliary heat exchanger flows to tar knock-out drum.
7. the method for claim 3, wherein step (c) comprises that the ejecta that lets from auxiliary heat exchanger flows to tar knock-out drum.
8. the method for claim 4, wherein step (c) comprises that the ejecta that lets from auxiliary heat exchanger flows to tar knock-out drum.
9. claim 1 or 2 method comprise step (d): with remove in the step (c) after the tar remaining ejecta further cooling with condensation pyrolysis naphtha therefrom with the temperature of this ejecta is reduced to less than 212 ° of F.
10. the method for claim 3 comprises step (d): with remove in the step (c) after the tar remaining ejecta further cooling with condensation pyrolysis naphtha therefrom with the temperature of this ejecta is reduced to less than 212 ° of F.
11. the method for claim 4 comprises step (d): with remove in the step (c) after the tar remaining ejecta further cooling with condensation pyrolysis naphtha therefrom with the temperature of this ejecta is reduced to less than 212 ° of F.
12. the method for claim 6 comprises step (d): with remove in the step (c) after the tar remaining ejecta further cooling with condensation pyrolysis naphtha therefrom with the temperature of this ejecta is reduced to less than 212 ° of F.
13. the method for claim 9 is wherein carried out step (d) through the direct quenching of water.
14. the method for claim 9 is wherein carried out step (d) through indirect heat exchange.
15. the method for claim 1 or 2 will be wherein through will the pyrolysis of ebullient hydrocarbon feed preparing said gaseous state ejecta in the TR of 104 ° of F-356 ° of F.
16. the method for claim 3 will be wherein through will the pyrolysis of ebullient hydrocarbon feed preparing said gaseous state ejecta in the TR of 104 ° of F-356 ° of F.
17. the method for claim 4 will be wherein through will the pyrolysis of ebullient hydrocarbon feed preparing said gaseous state ejecta in the TR of 104 ° of F-356 ° of F.
18. the method for claim 6 will be wherein through will the pyrolysis of ebullient hydrocarbon feed preparing said gaseous state ejecta in the TR of 104 ° of F-356 ° of F.
19. the method for claim 9 will be wherein through will the pyrolysis of ebullient hydrocarbon feed preparing said gaseous state ejecta in the TR of 104 ° of F-356 ° of F.
20. the method for claim 13 will be wherein through will the pyrolysis of ebullient hydrocarbon feed preparing said gaseous state ejecta in the TR of 104 ° of F-356 ° of F.
21. the method for claim 14 will be wherein through will the pyrolysis of ebullient hydrocarbon feed preparing said gaseous state ejecta in the TR of 104 ° of F-356 ° of F.
22. be used for the treatment process from the gaseous state ejecta of hydrocarbon pyrolytic process device, this method comprises:
(a) let this gaseous state ejecta pass at least one main heat exchanger, thereby cool off this gaseous state ejecta;
(b) let the said gaseous state ejecta from step (a) pass the auxiliary heat exchanger that at least one has heat exchange surface; This heat exchange surface maintains 300 ° of F to the temperature less than 599 ° of F; Make a part of condensation of this gaseous state ejecta on said surface, forming liquid coating, thereby further the remainder of this gaseous state ejecta is cooled to make the temperature of at least a portion condensation of the tar that forms by pyrolytic process in said gaseous state ejecta;
(c) let the ejecta from step (b) pass at least one knockout drum, there, the tar of condensation separates with the gaseous state ejecta; And then
(d) will be reduced to less than 212 ° of F from the temperature of the gaseous state ejecta of step (c).
23. the method for claim 22, wherein said heat exchange surface are substantially perpendicularly arranged and through maintaining under the said temperature with the heat-transfer medium indirect heat exchange that is downward through said at least one auxiliary heat exchanger.
24. the method for claim 22 or 23, wherein said heat exchange surface are through maintaining under the said temperature with the water indirect heat exchange, and the water that will in this at least one auxiliary heat exchanger, heat is as the heat exchange medium in this main heat exchanger.
25. the method for claim 22 or 23, wherein step (d) is reduced to 68 ° of F-122 ° of F with the temperature of gaseous state ejecta.
26. the method for claim 24, wherein step (d) is reduced to 68 ° of F-122 ° of F with the temperature of gaseous state ejecta.
27. the method for claim 22 or 23, wherein step (d) also comprises condensation and the pyrolysis naphtha that separates from ejecta.
28. the method for claim 24, wherein step (d) also comprises condensation and the pyrolysis naphtha that separates from ejecta.
29. the method for claim 25, wherein step (d) also comprises condensation and the pyrolysis naphtha that separates from ejecta.
30. the method for claim 22 or 23 will be wherein through will the pyrolysis of ebullient hydrocarbon feed preparing said gaseous state ejecta in the TR of 104 ° of F-356 ° of F.
31. the method for claim 24 will be wherein through will the pyrolysis of ebullient hydrocarbon feed preparing said gaseous state ejecta in the TR of 104 ° of F-356 ° of F.
32. the method for claim 25 will be wherein through will the pyrolysis of ebullient hydrocarbon feed preparing said gaseous state ejecta in the TR of 104 ° of F-356 ° of F.
33. the method for claim 27 will be wherein through will the pyrolysis of ebullient hydrocarbon feed preparing said gaseous state ejecta in the TR of 104 ° of F-356 ° of F.
34. hydrocarbon cracking equipment, it comprises:
(a) be used for hydrocarbon feed pyrolytic reactor drum, this reactor drum has outlet, and the gaseous state pyrolysis effluent leaves this reactor drum via this outlet;
(b) in these reactor outlet downstream and connected at least one main heat exchanger, this main heat exchanger is used to cool off this gaseous state ejecta;
(c) in these at least one main heat exchanger downstream and connected at least one auxiliary heat exchanger; This auxiliary heat exchanger is used for further cooling off said gaseous state ejecta; Said at least one auxiliary heat exchanger has heat exchange surface; This heat exchange surface in use maintains and makes a part of condensation of this gaseous state ejecta with under the temperature that forms liquid coating on the said surface, thereby the remainder of this gaseous state ejecta is cooled to make the temperature of at least a portion condensation of the tar that is formed by pyrolytic process in the said gaseous state ejecta; Wherein said at least one auxiliary heat exchanger comprises the inlet that is used for said gaseous state ejecta, and said inlet and said heat exchange surface are heat insulation said inlet is maintained greater than under the temperature that makes the tar condensing in the said gaseous state ejecta; The wherein said auxiliary heat exchanger of advocating peace comprises that the internal diameter that each heat transfer tube had of heat transfer tube and auxiliary heat exchanger is equal to or greater than the internal diameter of each heat transfer tube of main heat exchanger; With
(d) separate the tar of said condensation and the device of said gaseous state ejecta;
Wherein this hydrocarbon cracking equipment also comprises the decoking system with decoking medium inlet and coke export; The wherein said auxiliary heat exchanger of advocating peace is connected with said decoking system, makes said decoking medium pass said at least one main heat exchanger and pass said at least one auxiliary heat exchanger then to flow to said outlet then.
35. the equipment of claim 34, wherein said heat exchange surface are substantially perpendicularly arranged and through maintaining under the said temperature with the heat-transfer medium indirect heat exchange that is downward through said at least one auxiliary heat exchanger.
36. the equipment of claim 34 or 35, wherein said at least one auxiliary heat exchanger is shell and tube heat exchanger or double-pipe exchanger.
37. the equipment of claim 34 or 35 wherein is used to separate the tar of said condensation and the said device (d) of said gaseous state ejecta is a tar knock-out drum.
38. the equipment of claim 36 wherein is used to separate the tar of said condensation and the said device (d) of said gaseous state ejecta is a tar knock-out drum.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US11/178,158 | 2005-07-08 | ||
| US11/178,158 US7465388B2 (en) | 2005-07-08 | 2005-07-08 | Method for processing hydrocarbon pyrolysis effluent |
| PCT/US2006/024892 WO2007008397A1 (en) | 2005-07-08 | 2006-06-27 | Method for processing hydrocarbon pyrolysis effluent |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101218320A CN101218320A (en) | 2008-07-09 |
| CN101218320B true CN101218320B (en) | 2012-07-04 |
Family
ID=36649835
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2006800247671A Expired - Fee Related CN101218320B (en) | 2005-07-08 | 2006-06-27 | Method for processing hydrocarbon pyrolysis effluent |
Country Status (7)
| Country | Link |
|---|---|
| US (2) | US7465388B2 (en) |
| EP (1) | EP1922387A1 (en) |
| JP (1) | JP4777423B2 (en) |
| KR (1) | KR100966961B1 (en) |
| CN (1) | CN101218320B (en) |
| CA (1) | CA2609903C (en) |
| WO (1) | WO2007008397A1 (en) |
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| CN101113366B (en) * | 2007-07-17 | 2011-05-11 | 华东理工大学 | Hydrocarbons pyrolysis coking judgment pilot experimental device |
| US8074973B2 (en) * | 2007-10-02 | 2011-12-13 | Exxonmobil Chemical Patents Inc. | Method and apparatus for cooling pyrolysis effluent |
| US8105479B2 (en) * | 2009-06-18 | 2012-01-31 | Exxonmobil Chemical Patents Inc. | Process and apparatus for upgrading steam cracker tar-containing effluent using steam |
| US20120024749A1 (en) * | 2010-07-30 | 2012-02-02 | Strack Robert D | Method For Processing Hydrocarbon Pyrolysis Effluent |
| SG186168A1 (en) * | 2010-07-30 | 2013-01-30 | Exxonmobil Chem Patents Inc | Method for processing hydrocarbon pyrolysis effluent |
| US8921632B2 (en) * | 2010-08-10 | 2014-12-30 | Uop Llc | Producing 1-butene from an oxygenate-to-olefin reaction system |
| US8829259B2 (en) | 2010-08-10 | 2014-09-09 | Uop Llc | Integration of a methanol-to-olefin reaction system with a hydrocarbon pyrolysis system |
| FR3011556B1 (en) * | 2013-10-09 | 2015-12-25 | Commissariat Energie Atomique | PROCESS FOR PURIFYING A RAW SYNTHESIS GAS FROM A PYROLYSIS AND / OR GASIFYING A CHARGE OF CARBON MATERIAL BY DESTRUCTION OF TARS CONTAINED IN THE GAS |
| JP6467805B2 (en) * | 2014-08-07 | 2019-02-13 | 新日鐵住金株式会社 | Exhaust gas treatment method and exhaust gas treatment equipment for tar utilization equipment |
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| US20190293364A1 (en) * | 2018-03-22 | 2019-09-26 | Johnson Controls Technology Company | Varied geometry heat exchanger systems and methods |
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| EP0205205A1 (en) * | 1985-05-28 | 1986-12-17 | Dow Chemical (Nederland) B.V. | Transfer-line cooler |
| US6183626B1 (en) * | 1996-06-25 | 2001-02-06 | Institute Francais Du Petrole | Method and device for steam cracking comprising the injection of particles upstream of a secondary quenching exchanger |
Also Published As
| Publication number | Publication date |
|---|---|
| KR20080021765A (en) | 2008-03-07 |
| CA2609903C (en) | 2012-05-01 |
| EP1922387A1 (en) | 2008-05-21 |
| WO2007008397A1 (en) | 2007-01-18 |
| CN101218320A (en) | 2008-07-09 |
| US7465388B2 (en) | 2008-12-16 |
| KR100966961B1 (en) | 2010-06-30 |
| US7981374B2 (en) | 2011-07-19 |
| CA2609903A1 (en) | 2007-01-18 |
| JP4777423B2 (en) | 2011-09-21 |
| US20070007175A1 (en) | 2007-01-11 |
| US20090074636A1 (en) | 2009-03-19 |
| JP2009500492A (en) | 2009-01-08 |
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